|Publication number||US4871398 A|
|Application number||US 07/282,403|
|Publication date||Oct 3, 1989|
|Filing date||Dec 9, 1988|
|Priority date||Dec 9, 1988|
|Also published as||CA2000827A1, CA2000827C, CN1043320A|
|Publication number||07282403, 282403, US 4871398 A, US 4871398A, US-A-4871398, US4871398 A, US4871398A|
|Inventors||Jay H. Katcher, John T. Mabon, Jennifer W. Matherly, Lawrence T. McCarty, Robert E. Schara|
|Original Assignee||General Foods Corporation|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (6), Non-Patent Citations (2), Referenced by (22), Classifications (9), Legal Events (4)|
|External Links: USPTO, USPTO Assignment, Espacenet|
Processes for producing spray-dried pregelatinized starch have been disclosed in U.S. Pat. No. 4,280,851 to Pitchon et al. This patent, which is hereby incorporated by reference, discloses a process wherein an aqueous starch slurry is injected through one or more centrally-located atomization apertures in a two-fluid nozzle to form a relatively fine-sized spray. A heating medium (e.g. steam) is also injected through other apertures in the nozzle and into the spray of atomized starch slurry so as to heat the starch to a temperature which is effective to gelatinize the starch. An enclosed chamber surrounds the atomization and heating medium injection apertures and defines a vent aperture which is positioned to enable the heated, atomized starch spray to exit the chamber. The chamber is sized such that the elapsed time for passage of the spray droplets through the chamber (i.e., from the atomization aperture through the vent aperture) is sufficient to effect gelatinization of the starch. The major portion of gelatinization occurs within the chamber; however, some gelatinization may occur upon the exiting of the spray from the enclosed chamber, as a result of the heat and moisture that is carried from the chamber. Thus, gelatinization time includes both time within the chamber as well as the period of time outside of the chamber during which the starch retains a temperature and moisture which can effect gelatinization.
The Pitchon et al. patent further discloses that the spray from the enclosed chamber passes into a spray-drying tower where the spray particles are dried in a stream of heated air. This patent also discloses that a plurality of nozzles may be uniformly-spaced around the top of a single spray-drying tower in order to increase the amount of spray-dried, pregelatinized starch material which is produced. The dried, pregelatinized starch produced in accordance with the Pitchon et al. patent is described as having a mesh size wherein about 80% by weight of the starch passes through a 230 mesh U.S. Standard Screen, with the particles being in the form of loosely-bound agglomerates of starch granules, the granules being in the form of indented spheres and the agglomerates separating into individual granules upon dispersion in water.
The spray-dried starch material produced by the process of the Pitchon et al. patent has been found to contain both an exceedingly wide range of particle sizes and a high percentage of fine particles (e.g., 55% by weight of the particles being less than 53 microns or minus 270 U.S. mesh). It is desirable to produce a spray-dried pregelatinized starch material which has a relatively narrow particle size distribution. Such a material could more readily be optimized to meet the preferred particle size requirements of a given starch-containing, dry mix. It is also desirable to obtain a spray-dried pregelatinized starch material which has a reduced level of fine (minus 270 U.S. mesh) particles. This will improve the dispersibility of the starch when a dry-blended mix containing the starch is mixed with a cold, aqueous fluid, such as when instant pudding mixes ar combined with milk.
Of course, it is known to adjust particle size distribution and reduce the level of fines in a particulate material by means of agglomeration. Fine starch powders are typically agglomerated using balling or tumbling techniques wherein a liquid binder is sprayed onto an agitated bed of dry starch powder. The liquid dissolves the surface of the starch particles and liquid bridges are formed between solid particles which bridges, upon drying, become a solid bond. Such agglomeration techniques, however, require separate agglomeration equipment and processing and thus add to production costs.
The present invention is directed to a continuous process for producing gelatinized, spray-dried and agglomerated starch which has a relatively narrow particle-size distribution and a relatively low level of fine particles. The objects of this invention are achieved by means of a specially designed spray nozzle system which produces agglomerated, pregelatinized, spray-dried starch without the need for separate agglomeration equipment.
When operating in accordance with this invention it is possible to obtain spray-dried starch material which has a particle size distribution with a reduced level of minus 270 U.S. mesh (i.e., less than 53 micron) particles. The starch material produced in accordance with the spray-drying process of this invention will typically contain agglomerates sized up to about 200 microns. As it is desirable to keep the plus 120 U.S. mesh (above 125 microns) particles to a minimum in order to improve the texture of any pudding-like product containing the starch, it will be desirable to screen out the +120 mesh starch agglomerates. This oversized material may be readily ground using conventional grinding equipment, such as a micropulverizer, an air classifying mill or the like, to a particle size distribution wherein essentially all of the ground material is +270 and -120 mesh. This ground starch material may if necessary, be screened through a 120 U.S. mesh screen and then be combined with the main product stream.
According to this invention, two or more capped, two-fluid nozzles, of the type described in the aforementioned Pitchon et al. patent, are positioned within a spray-drying tower so that their spray patterns intersect at a desired location. The positioning of nozzles must be such that contact of the particles occurs at a location where the particle surface are tacky enough to promote adherence of the particles but not so close to the nozzle vent apertures that globbing or clumping of the starch particles occur.
FIG. 1 is an elevational sectional view of a two-fluid nozzle which is useful in this invention.
FIG. 2 is a top plan view of two nozzles, of the type shown in FIG. 1, positioned within a circular spray-drying tower.
FIG. 3 is an elevational view of FIG. 2 also showing intersecting spray patterns forming an agglomeration zone.
FIG. 1 illustrates in elevation a cross-sectional view of a two-fluid, capped nozzle 10 which is useful in the practice of this invention. In this embodiment of a nozzle, the aqueous starch slurry, typically having a solids content of from 30 to 42% by weight, enters nozzle 10 through conduit 11 and is first directed radially inwardly and then axially downward through an atomization aperture 12 formed in the central portion of the nozzle 10 into a spinner and orifice 13 arranged in the lower portion of the atomization aperture 12. The spinner and orifice 13 assist in atomizing the material so as to convert the starch slurry into a fine, cone-shaped spray. The viscosity of the uncooked starch slurry is initially low, and this allows for the atomization of the material by such means as a small orifice and spinner, and results in the production of a relatively fine spray. These spray particles will be spherical and typically have a diameter of from about 20 to 200 microns. Steam (or other heating medium) enters through a conduit 14 and enters an annular manifold 15 positioned about the longitudinally-extending atomization aperture 12. The annular manifold is gradually reduced in diameter towards its lower end forming an annular heating medium interjection aperture 16. From the heating medium interjection aperture 16, the steam is interjected into the atomized starch slurry being sprayed from the atomization aperture 12.
A nozzle cap 17 encloses the atomization and heating medium interjection apertures (12 and 16 respectively). The nozzle cap 17 contains a vent aperture 18 which is positioned opposite the atomization and heating medium apertures. The enclosed area between the nozzle cap 17 and the atomization and heating medium apertures forms the enclosed chamber wherein the heating medium is interjected into the spray of atomized starch slurry to gelatinize the starch. The size and shape of the chamber and vent aperture is effective to maintain the temperature and moisture content of the starch for a period of time sufficient to gelatinize the starch. The enclosed chamber maintains a desired temperature and moisture content to enable the starch to be uniformly gelatinized.
Pressures to and flow rates through conduits 11 and 14, as well as the sizing of the apertures and nozzle cap, will be readily determined by those skilled in the art having reference to the aforementioned Pitchon, et al. patent.
FIGS. 2 and 3 illustrate a single set of two nozzles within a spray-drier. The nozzles 10 and 10' are shown as being positioned at an off-center location within the circular spray-drying tower 20; however, this invention is not limited to this arrangement. A set of nozzles could contain more than two nozzles; however, a set will usually not exceed four nozzles. The spray-drying tower could, depending on its diameter, accommodate a plurality of nozzle sets.
Within a given set of nozzles, the starch slurry may be supplied to each nozzle through a common supply conduit 21. Steam is supplied to each nozzle through one or more steam lines. As shown in FIG. 2, each nozzle 10 and 10' is connected to separate steam lines 14 and 14'. Of course, a single steam line could supply steam to both nozzles provided an adequate amount of steam enter each of the nozzles. Preferably, nozzles are selected which provide full-cone spray patterns, typically having a circular shape. The nozzles are oriented so that the spray patterns fully intersect or overlap. This may be accomplished by angling each of the nozzles toward each other or, as shown in FIG. 3, maintaining one nozzle 10' perpendicular and angling the other nozzle or nozzles within the set. When performing the process of this invention, nozzles within a set should be aligned such that the angle at which the spray patterns intersect is between less than 120 and greater than 30 degrees. Preferably, this angle will be in the range of 45 to 90 degrees. As a result of the agglomeration process of this invention, it has been possible to obtain pregelatinized starch material directly from the spray drier wherein at least 65% by weight of the spray-dried material is between 53 microns (270 U.S. mesh) and 125 microns (120 U.S. mesh) and wherein the spray-dried material is essentially-free of particles smaller than 53 microns (270 U.S mesh).
In accordance with this invention, an atomized spray of gelatinized starch exits the cooking chamber. As the spray particles dry, they develop a tacky, semi-solid surface. It is at this point that the spray patterns are caused to intersect so that contact between the tacky surfaces of the particles causes adhesion by acting as a semi-liquid binder. As drying proceeds, solid bonds are formed between the spray particles. If the spray patterns intersect to soon, wet particles will coalesce leading to dense globs which are both difficult to dry and will not hydrate rapidly enough to be suitable for use in instant food mixes, such as instant puddings. If the spray patterns intersect too late, the particle surfaces will be too dry to effect adhesion and little or no agglomeration will occur.
The agglomerated starch particles which are produced must be strong enough to hold up under conveying, shipping and mixing. The agglomerates, however, must be weak enough that, upon mixing with cold milk or water, they will readily break up and disperse, so that, in the case of an instant pudding mix, the prepared pudding will have a smooth, creamy texture and a glossy surface. Guided by these criteria one skilled in the art will, without undue difficulty, be able to adjust parameters such as the angle of intersection, the temperature of the heated air into which the particles are sprayed and the height of the spray-drying tower in order to obtain the desired spray-dried starch agglomerates. The agglomerates are dried to a moisture content of between 3 and 9% by weight.
This invention is further described but not limited by the following Example.
A set of two nozzles was mounted in a spray tower. The nozzles, which were of design generally in accordance with the nozzle depicted in FIG. 1, were placed at the same elevation, about 6 inches apart and positioned so that their spray patterns intersected at an angle of 60░. The nozzles were positioned far enough away from the walls of the tower that essentially no spray contacted the tower walls. A corn starch slurry of 40% solids was fed to the nozzles via a high pressure pump at 2500 psig. and at a rate of 2.5 gallons per minute (9.46 l/min) per nozzle. Steam was introduced into the nozzles at 150 psig. The atomization-aperture contained a spinner and orifice having a spinner with 4 grooves of 0.025 inches (0.64 mm) wide and 0.048 inches deep and having an orifice size of 0.042 inches (1.07 mm). The distance between the atomization aperture and the nozzle vent aperture was 0.875 inches (22 mm) with the vent aperture having a diameter of 0.25 inches (6.4 mm).
The spray tower was operated in a co-current manner with an air inlet temperature of 450░ F. (232.2░ C.), an air outlet temperature of 180░ F. (82░ C.) and an air flow rate, as measured at the fan exhaust, of 25,000 cubic feet per minute (703.7 cubic meter/min.). The starch exiting the tower had a moisture content of about 5% by weight and a particle size distribution where 66 to 73% by weight of the particles were between 53 and 125 microns, with about 30% by weight of the remaining particles being in excess of 125 microns and with little or no starch smaller than 53 microns. The +125 micron particles were then ground to proper particle size.
By way of comparison a similar run was conducted with both nozzles being and aligned vertically in the tower so that there were no intersecting spray patterns. The resulting dried particles had a particle size distribution wherein only 58 to 64% by weight of the particles were between 53 and 125 microns. Significant amounts of material (about 15 to 25% by weight) was less than 53 microns and about 15 to 20% by weight of the material was in excess of 125 microns.
An instant pudding mix was prepared as follows:
______________________________________ EXAMPLE 2An instant pudding mix was prepared as follows:Ingredient Grams______________________________________Sucrose 75.7Spray-Dried Starch of Example 1 18.0Sodium Phospate 3.5Salt 0.5Mono and Diglyceride Emulsifier 0.5Vegetable Oil 0.4Flavor and Color 0.6______________________________________
This mix was blended with 473 ml. of cold milk using an electric blender. This mix readily dispersed and the pudding was allowed to set. The resulting pudding had a smooth, creamy texture and a glossy surface appearance.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US3039107 *||Mar 10, 1961||Jun 12, 1962||Swift & Co||Agglomeration of spray-dried materials|
|US3083099 *||Aug 24, 1959||Mar 26, 1963||Wisconsin Alumni Res Found||Agglomeration process|
|US3121639 *||Oct 19, 1960||Feb 18, 1964||Dairy Foods Inc||Spray drying process|
|US3276907 *||Sep 27, 1965||Oct 4, 1966||Union Starch & Refining Co Inc||Continuous production of industrial starch pastes|
|US4280851 *||Dec 14, 1979||Jul 28, 1981||General Foods Corporation||Process for cooking or gelatinizing materials|
|US4469712 *||Jan 10, 1983||Sep 4, 1984||General Foods Corporation||Dry instant pudding mix|
|1||*||Masters, K., Spray Drying, Second Edition pp. 554, 563, 595 596 (Wiley & Sons 1976).|
|2||Masters, K., Spray Drying, Second Edition pp. 554, 563, 595-596 (Wiley & Sons 1976).|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US5188674 *||May 8, 1991||Feb 23, 1993||National Starch And Chemical Investment Holding Corporation||Continuous coupled jet-cooking/spray-drying process and novel pregelatinized high amylose starches prepared thereby|
|US5281432 *||Jun 2, 1992||Jan 25, 1994||National Starch And Chemical Investment Holding Corporation||Method of making foods containing soluble high amylose starch|
|US5318635 *||Jul 27, 1992||Jun 7, 1994||National Starch And Chemical Investment Holding Corporation||Continuous coupled jet-cooking/spray-drying process and novel pregelatinized high amylose starches prepared thereby|
|US5435851 *||May 9, 1994||Jul 25, 1995||National Starch And Chemical Investment Holding Corporation||Continuous coupled jet-cooking/spray-drying process and novel pregelatinized high amylose starches and gums prepared thereby|
|US5571552 *||Apr 6, 1995||Nov 5, 1996||National Starch And Chemical Investment Holding Corporation||Continuous coupled jet-cooking/spray-drying process and novel pregelatinized high amylose starches and gums prepared thereby|
|US5597603 *||Feb 28, 1995||Jan 28, 1997||Kraft Foods, Inc.||Sugar-free, fat-free instant pudding mix|
|US5738900 *||Aug 30, 1996||Apr 14, 1998||Kraft Foods, Inc.||Process for making a readily-dispersible, dry food mix|
|US6287621||Oct 17, 1996||Sep 11, 2001||National Starch And Chemical Investment Holding Corporation||Sweetened extruded cereals containing pregelatinized high amylose starches|
|US7819977||Feb 19, 2004||Oct 26, 2010||Syram Belgium nv||Spray-dried starch hydrolysate agglomerate product and method for preparing a spray-dried starch hydrolysate agglomerate product|
|US9724302||Mar 5, 2013||Aug 8, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US9730892||Aug 26, 2016||Aug 15, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US9737482||Mar 6, 2013||Aug 22, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US9737483||Mar 6, 2013||Aug 22, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US9757336||Mar 6, 2013||Sep 12, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US9808424||Mar 8, 2013||Nov 7, 2017||Pacira Pharmaceuticals, Inc.||Method for formulating large diameter synthetic membrane vesicles|
|US20070190228 *||Feb 19, 2004||Aug 16, 2007||Helena Vanhoutte||Spray-dried starch hydrolysate agglomerate product and method for preparing a spray-dried starch hydrolysate agglomerate product|
|EP0428232A1 *||Nov 14, 1990||May 22, 1991||Verenigde Co÷peratieve Melkindustrie Coberco B.A.||A process for batchwise preparing a liquid having increased viscosity on the basis of milk|
|EP0438783A2 *||Dec 27, 1990||Jul 31, 1991||National Starch and Chemical Investment Holding Corporation||Method and apparatus for cooking and spray-drying starch|
|EP0438783A3 *||Dec 27, 1990||Jan 8, 1992||National Starch And Chemical Investment Holding Corporation||Method and apparatus for cooking and spray-drying starch|
|EP0480433A2 *||Oct 10, 1991||Apr 15, 1992||National Starch and Chemical Investment Holding Corporation||Foods containing soluble high amylose starch|
|EP0480433A3 *||Oct 10, 1991||Jul 28, 1993||National Starch And Chemical Investment Holding Corporation||Foods containing soluble high amylose starch|
|WO2005079595A1 *||Feb 19, 2004||Sep 1, 2005||Tate & Lyle Europe Nv||Spray-dried starch hydrolysate agglomerate product and method for preparing a spray-dried starch hydrolysate agglomerate product|
|U.S. Classification||127/71, 127/32, 127/69|
|International Classification||C08B30/16, C08B30/14|
|Cooperative Classification||C08B30/14, C08B30/16|
|European Classification||C08B30/16, C08B30/14|
|Aug 3, 1989||AS||Assignment|
Owner name: GENERAL FOODS CORPORATION, NEW YORK
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNORS:KATCHER, JAY H.;MABON, JOHN T.;MATHERLY, JENNIFER W.;AND OTHERS;REEL/FRAME:005136/0098;SIGNING DATES FROM 19890112 TO 19890203
|Apr 2, 1993||FPAY||Fee payment|
Year of fee payment: 4
|Apr 2, 1997||FPAY||Fee payment|
Year of fee payment: 8
|Apr 2, 2001||FPAY||Fee payment|
Year of fee payment: 12